JP2008508099A - Co2の除去を包含する燃焼ガスの超清浄化 - Google Patents
Co2の除去を包含する燃焼ガスの超清浄化 Download PDFInfo
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- B01D—SEPARATION
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Abstract
Description
‐MEA剤は高価であり、酸素及びCO2雰囲気において劣化する。
‐MEAは腐食性であり、比較的希薄な性状でのみ使用される。
‐MEAとCO2との反応は、高度に発熱性である。
‐再生がエネルギー大量消費性である。
‐プロセスが熱及び補助電力の大量消費性である。
‐残留汚染物を捕捉する、
‐CO2を捕捉し、金属イオン封鎖用に濃縮及び高圧形でCO2を放出する、
との要求がある。
CO2(ガス)→ CO2(水溶液)
CO2(水溶液)+ H2O → H+ + HCO3 -
(NH4)2CO3(固体) → 2NH4 + + CO3 2-
H+ + CO3 2- → HCO3 -
HCO3 - + NH4 + → NH4HCO3(固体)
上記反応において、ガスから捕捉されたCO2は、炭酸アンモニウムを炭酸水素アンモニウムに転化する。上記反応は可逆性であり、CO2は、高温において、液相からストリップされる。
NH4 + + CO3 2- → NH3(ガス)+ HCO3 -
NH4 + + HCO3 - → NH3(ガス)+CO2(ガス)+H2O
上記反応により、ガス相へのNH3の放出が生ずる。吸収器におけるより低い温度及びより低いNH3/CO2比は、これら不要の反応を抑制する。しかし、再生の間及び高温では、ガス状のアンモニアが形成される。液相からアンモニアが消失することを防止するため(及び他の理由により)、再生器は、高圧及び溶液におけるアンモニアの溶解度が非常に高く、ガス状アンモニアの放出が非常に低い条件下で作動されるようになっている。
Claims (32)
- 汚染燃焼ガスを超清浄化するためのシステムであって、
(a)ガスストリームを冷却して、前記ガスストリームから水を凝縮させ、かつ前記ガスストリームから汚染物を捕捉及び除去するために、1以上の直接かつ湿式の冷却ステージを持つ冷却サブシステム;
(b)アンモニア処理溶液又はスラリーを使用することによって、前記の冷却されたガスストリームからCO2を吸収するために、1以上のCO2吸収ステージを持つ吸収サブステージ;及び
(c)前記の吸収されかつアンモニアと化合したCO2からCO2を分離するために、1以上のCO2再生ステージを持つ再生サブシステム
を包含することを特徴とする、汚染燃焼ガスの超清浄化システム。 - 冷却サブスシステムが、ガスストリームを約0−20℃に冷却する、請求項1記載のシステム。
- 冷却サブスシステムが、ガスストリームを約0−10℃に冷却する、請求項1記載のシステム。
- CO2を、CO2希薄NH3−CO2−H2O溶液又はスラリーにて吸収する、請求項1記載のシステム。
- CO2希薄溶液又はスラリーが、1.5−4.0の範囲のモル比NH3/CO2を有する、請求項4記載のシステム。
- CO2希薄溶液又はスラリーが、1.5−3.0の範囲のモル比NH3/CO2を有する、請求項4記載のシステム。
- 吸収サブシステムが、0−20℃の範囲の温度で作動する、請求項1記載のシステム。
- 吸収サブシステムが、0−10℃の範囲の温度で作動する、請求項1記載のシステム。
- 吸収サブシステムが、CO2富有NH3−CO2−H2O溶液を生成する、請求項1記載のシステム。
- CO2富有溶液が、1.0−2.0の範囲のモル比NH3/CO2を有する、請求項9記載のシステム。
- CO2富有溶液が、1.0−1.5の範囲のモル比NH3/CO2を有する、請求項9記載のシステム。
- 再生サブシステムが、50−200℃の範囲の温度で作動する、請求項1記載のシステム。
- 再生サブシステムが、100−150℃の範囲の温度で作動する、請求項1記載のシステム。
- 再生サブシステムが、30−2000 psiの範囲の圧力で作動する、請求項1記載のシステム。
- 再生サブシステムが、150−400 psiの範囲の圧力で作動する、請求項1記載のシステム。
- 汚染燃焼ガスを超清浄化する方法であって、
(a)1以上の直接かつ湿式の冷却ステージにてガスストリームを冷却して、前記ガスストリームから水を凝縮させ、かつ前記ガスストリームから汚染物を捕捉及び除去する工程;
(b)1以上のCO2吸収ステージにて、アンモニア処理溶液又はスラリーを使用して、前記の冷却されたガスストリームからCO2を吸収する工程;及び
(c)1以上のCO2再生ステージにて、前記の吸収されかつアンモニアと化合したCO2からCO2を分離する工程;
を包含することを特徴とする、汚染燃焼ガスの超清浄化法。 - 冷却工程を、0−20℃の範囲の温度で行う、請求項16記載の方法。
- 冷却工程を、0−10℃の範囲の温度で行う、請求項16記載の方法。
- CO2を、CO2希薄NH3−CO2−H2O溶液又はスラリーにて吸収する、請求項16記載の方法。
- CO2希薄溶液又はスラリーが、1.5−4.0の範囲のモル比NH3/CO2を有する、請求項19記載の方法。
- CO2希薄溶液が、1.5−3.0の範囲のモル比NH3/CO2を有する、請求項19記載の方法。
- NH3−CO2−H2O溶液又はスラリー中の化学種が、水に溶解した形である、請求項19記載の方法。
- NH3−CO2−H2O溶液又はスラリー中の化学種を、炭酸アンモニウム((NH4)2CO3)、及び炭酸水素アンモニウム(NH4HCO3)の塩を有する溶解又は懸濁化固体を含有するように濃縮する、請求項16記載の方法。
- 吸収工程を、0−20℃の範囲の温度で行う、請求項16記載の方法。
- 吸収工程を、0−10℃の範囲の温度で行う、請求項16記載の方法。
- 吸収工程が、CO2富有NH3−CO2−H2O溶液を生成する、請求項16記載の方法。
- CO2富有溶液が、1.0−2.0の範囲のモル比NH3/CO2を有する、請求項26記載の方法。
- CO2富有溶液が、1.0−1.5の範囲のモル比NH3/CO2を有する、請求項26記載の方法。
- 再生工程を、50−200℃の範囲の温度で行う、請求項16載の方法。
- 再生工程を、100−150℃の範囲の温度で行う、請求項16記載の方法。
- 再生工程を、30−2000 psiの範囲の圧力で行う、請求項16記載の方法。
- 再生工程を、150−400 psiの範囲の圧力で行う、請求項16載の方法。
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PCT/US2005/012794 WO2006022885A1 (en) | 2004-08-06 | 2005-04-12 | Ultra cleaning of combustion gas including the removal of co2 |
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JP2016540626A (ja) * | 2013-10-07 | 2016-12-28 | リード システムズ(オーストラリア) ピーティーワイ エルティーディーReid Systems (Australia) Pty Ltd | 排煙から二酸化炭素を除去する方法および装置 |
JP2018538394A (ja) * | 2015-11-27 | 2018-12-27 | ポスコPosco | 酸性ガス内の二酸化炭素除去方法およびその装置 |
JP2018134604A (ja) * | 2017-02-23 | 2018-08-30 | 川崎重工業株式会社 | 二酸化炭素分離回収システム |
Also Published As
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US8308849B2 (en) | 2012-11-13 |
US20100064889A1 (en) | 2010-03-18 |
EP1781400B1 (en) | 2013-07-03 |
IL180614A0 (en) | 2007-06-03 |
BRPI0514141A (pt) | 2008-05-27 |
DK1781400T3 (da) | 2013-09-23 |
US20080072762A1 (en) | 2008-03-27 |
RU2378040C2 (ru) | 2010-01-10 |
AU2005278126B2 (en) | 2010-08-19 |
IL180614A (en) | 2012-01-31 |
PL1781400T3 (pl) | 2013-11-29 |
WO2006022885A1 (en) | 2006-03-02 |
CA2574633A1 (en) | 2006-03-02 |
AU2005278126A1 (en) | 2006-03-02 |
NO335509B1 (no) | 2014-12-22 |
JP4995084B2 (ja) | 2012-08-08 |
EP1781400A4 (en) | 2009-07-15 |
KR100869665B1 (ko) | 2008-11-21 |
KR20070053738A (ko) | 2007-05-25 |
CA2574633C (en) | 2010-08-10 |
EP1781400A1 (en) | 2007-05-09 |
US7641717B2 (en) | 2010-01-05 |
RU2007108285A (ru) | 2008-09-20 |
NO20070165L (no) | 2007-05-07 |
MX2007001367A (es) | 2007-04-10 |
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